EP3289050B1 - Four à pyrolyse - Google Patents

Four à pyrolyse Download PDF

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Publication number
EP3289050B1
EP3289050B1 EP16724595.0A EP16724595A EP3289050B1 EP 3289050 B1 EP3289050 B1 EP 3289050B1 EP 16724595 A EP16724595 A EP 16724595A EP 3289050 B1 EP3289050 B1 EP 3289050B1
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EP
European Patent Office
Prior art keywords
pyrolysis
condenser
furnace
fuser
disaggregation
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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EP16724595.0A
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German (de)
English (en)
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EP3289050A1 (fr
Inventor
Domenico TANFOGLIO
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Individual
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Individual
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Priority claimed from ITUB2015A005217A external-priority patent/ITUB20155217A1/it
Priority claimed from ITUB2015A004810A external-priority patent/ITUB20154810A1/it
Priority claimed from ITUB2015A004809A external-priority patent/ITUB20154809A1/it
Priority claimed from ITUB2015A005142A external-priority patent/ITUB20155142A1/it
Priority claimed from ITUB2015A005060A external-priority patent/ITUB20155060A1/it
Application filed by Individual filed Critical Individual
Priority claimed from PCT/EP2016/059696 external-priority patent/WO2016174247A1/fr
Publication of EP3289050A1 publication Critical patent/EP3289050A1/fr
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Publication of EP3289050B1 publication Critical patent/EP3289050B1/fr
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/007—Screw type gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C10G2300/1014—Biomass of vegetal origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/20—Feeding/conveying devices
    • F23K2203/201—Feeding/conveying devices using pneumatic means
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K2203/00—Feeding arrangements
    • F23K2203/20—Feeding/conveying devices
    • F23K2203/203—Feeding/conveying devices using pistons or rams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B9/00—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity
    • F27B9/14—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment
    • F27B9/16—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment the charge moving in a circular or arcuate path
    • F27B9/18—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment the charge moving in a circular or arcuate path under the action of scrapers or pushers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B9/00—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity
    • F27B9/14—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment
    • F27B9/16—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment the charge moving in a circular or arcuate path
    • F27B9/18—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment the charge moving in a circular or arcuate path under the action of scrapers or pushers
    • F27B9/185—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment the charge moving in a circular or arcuate path under the action of scrapers or pushers multiple hearth type furnaces
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/143—Feedstock the feedstock being recycled material, e.g. plastics
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the present invention relates to systems of pyrolysis disaggregation.
  • a plasma waste converter basically is a plasma torch applied to garbage.
  • a plasma torch uses a gas and powerful electrodes to create an ionized gas or plasma, i.e., a gas with free-roaming electrons that carries a current and generates a magnetic field.
  • ionized gas or plasma i.e., a gas with free-roaming electrons that carries a current and generates a magnetic field.
  • molecules break down in a process that may be referred to as molecular dissociation.
  • the molecular bonds holding them together become excited and break apart into their elemental components.
  • Organic, or carbon-based, molecules become volatized, or turn into gases referred to as synthetic gas or syngas, which can be used as a fuel source.
  • Inorganic compounds melt down and become vitrified, or converted, into a hard, glassy substance similar in appearance and weight to obsidian.
  • Metals melt down as well, combining with the rest of the inorganic matter (also referred to as "slag").
  • Plasma torches can operate in airtight vessels. Combustion requires oxidization; pyrolysis does not.
  • the heat, for example 500°C to 1100°C, from plasma converters causes pyrolysis, which is a process in which organic matter is broken down into non-condensable gases (CO, H2, CO2), non-condensable hydrocarbons (CH4, C2H6, C3H8, C4H10), heavy hydrocarbons, tars condensable in oils, water (H2O) and coke (carbon).
  • One method for achieving pyrolysis is to heat an organic material in a furnace by means of a double envelope in which combustion gases from a burner circulate. Since the heat is exchanged only by the walls, the method requires large surfaces and a large volume. It is useful for slow reactions conducted at low temperatures (400 to 500°C), but the temperatures and the mixing are not under good control and production cannot be switched from gas or oil production by user choice.
  • Another conventional method is direct heating of the material by hot gases released by a flame. Since the combustion in this method is in the same enclosure as the pyrolysis reaction a large oxygen supply is needed, which harms the quality of the waste gases. Accordingly, additional methods and systems may be desired.
  • U.S. Patent No. 8,308,912 disclosed another system and method in which high temperature stainless steel toroids are mixed with organic material in a small vertical furnace.
  • the stainless steel toroids may be an alloy containing nickel and cobalt, which may improve the gasification catalytically.
  • a system for pyrolysis using a furnace and a condenser is also described in US 2012/0073199 A1 as well as in US 2013/0240343 .
  • Plasma waste converters can treat almost any kind of waste, including some traditionally difficult waste materials. It can treat medical waste or chemically-contaminated waste and leave nothing but gases and slag. Because it breaks down these dangerous wastes into their basic elements, they can be disposed of safely.
  • the solid product reportedly contained more than 80 wt % elemental carbon, had a surface area of about 65 m2/g, and was referred to as pyrolytic carbon black (CBp).
  • CBp pyrolytic carbon black
  • XPS X-ray photoelectron spectroscopy
  • the CBp may be used as semi-reinforcing carbon black in non-tire rubber applications, or, after upgrading, as carbon black filler for tire.
  • the invention provides a system according to claims 1 and 11.
  • the system comprises of a pyrolysis disaggregation apparatus, henceforth abbreviated as pyrodisaggregator, a loading column, a thermal propeller, and a condenser.
  • the pyrodisaggregator is comprised of a furnace having a chamber within it, a fuser tube within the furnace chamber, an Archimedes screw within the fuser tube for moving material to be disaggregated through the fuser tube, a first furnace exit for inert materials from the fuser tube, a second furnace exit for gases from the fuser tube and a third furnace exit for fumes circulating through the furnace chamber.
  • the fuser tube may be substantially horizontal within the furnace chamber, although other orientations may also be used.
  • the fuser tube is connected to the first exit and the second exit.
  • a loading column is connected to the pyrodisaggregator for loading materials to be disaggregated into the fuser tube in the furnace.
  • a source of hot fumes produced by combustion is connected to the furnace, wherein hot fumes from the source circulate in the chamber is the furnace around the fuser tube.
  • the source of hot fumes may be a thermal propeller.
  • the system further may comprise a condenser connected to the second exit.
  • the condenser has an entry dome or other entry structure connected to the second exit from the furnace for receiving gases from the pyrodisaggregator, a cold water chamber surrounding the entrance dome for cooling the gases received from the pyrodisaggregator, a primary hopper connected to the entrance dome for collecting oil condensed out of the gases received from the pyrodisaggregator, first and second vertical condenser columns for proving a cooled path for gas flowing into the condenser column, each condenser column having a channel through which gases flow and an air lock space for water used to cool gases within the channel, a connection manifold connecting the first condenser column to the second condenser column, wherein gas from the entry dome flows into and through the first condenser column then through the connection manifold and then through the second condenser column, a secondary hopper connected to the second condenser column for receiving light hydrocarbons from the second condenser column, and an aspirator for moving Syngas from the condenser into a storage tank
  • the thermal propeller may comprise a combustion and pyrolysis chamber formed by at least one side wall, a primary fuser slab and a secondary fuser slab forming a bottom of the combustion and pyrolysis chamber, the primary fuser slab positioned to receive solid fuel from the loading column and the secondary fuser slab positioned to receive solid fuel from the primary fuser slab and a lid for closing the combustion and pyrolysis chamber.
  • the thermal propeller further may have a first agitator for moving solid fuel on the primary fuser slab and a second agitator for moving solid fuel on the secondary fuser slab. Still further, the thermal propeller may have a stoichiometric air carburetor connected to the combustion and pyrolysis chamber.
  • the stoichiometric air carburetor may have one or more exits into the combustion and pyrolysis chamber in an upper portion of the combustion and pyrolysis chamber.
  • the thermal propeller further may have a turbine driven fan connected to the stoichiometric air carburetor.
  • the thermal propeller may further comprise a first lower chamber beneath the primary fuser slab, wherein a plurality of air holes extend through the primary fuser slab wherein the stoichiometric air carburetor is connected to the first lower chamber.
  • the thermal propeller further may have an ash downloading exit.
  • the thermal propeller further may have a second lower chamber beneath the secondary fuser slab, wherein a plurality of air holes extend through the secondary fuser slab, wherein the second lower chamber is connected to the first lower chamber.
  • a molecular pyrodisaggregation system in another embodiment, includes a plurality of fuser tubes.
  • the system has a pyrodisaggregator, having a furnace, the furnace having a furnace wall defining a chamber within the furnace, a plurality of fuser tubes within the furnace chamber, a channel within the furnace chamber surrounding the plurality of fuser tubes, an Archimedes screw within each the fuser tubes for moving material to be disaggregated through the fuser tube, a first exit from each fuser tube for inert materials from the fuser tube, a second exit from each fuser tube for gases from the fuser tube, and a third exit from fumes circulating through the channel in the furnace.
  • a loader is connected to the pyrodisaggregator for loading materials to be disaggregated into the plurality of fuser tubes in the furnace.
  • a source of hot fumes is connected to the furnace, wherein hot fumes from the heat source circulate in the channel in the furnace around the fuser tubes.
  • a condenser connected to the second exit.
  • the condenser has an entrance dome connected to the second exit from the furnace for receiving gases from the pyrodisaggregator, a cold water chamber surrounding the entrance dome for cooling the gases received from the pyrodisaggregator.
  • First and second condenser columns each for proving a cooled path for gas flowing into the condenser columns.
  • Each condenser column has a plurality of spirals within the each condenser column for slowing a flow of gas within the condenser column, an air lock space within each the condenser columns for circulating water used to cool gas.
  • a connection manifold connects the first condenser column to the second condenser column, wherein gas from the entry dome flows into and through the first condenser column then through the connection manifold and then through the second condenser column, a primary hopper connected to the entrance dome and the first condenser column for collecting oil condensed out of the gases received from the pyrodisaggregator, a secondary hopper connected to the second condenser column for receiving light hydrocarbons from the second condenser column.
  • the condenser further has an aspirator for moving Syngas from the condenser into a storage tank.
  • the molecular pyrodisaggregation system 100 has a heat source or thermal propeller 200, a loading column 300, a disaggregator 400, a condenser 500 and a catalyst ion junction cube 600.
  • Organic material to be disaggregated is loaded into the system via loading column 300.
  • the loading column 300 which is described in more detail below with reference to FIG. 3 , air is removed from the organic material. From the loading column 300, the organic material, now void of air, is inserted into fuser tubes or pipes in the disaggregator 400 by an Archimedes screw.
  • a valve in the loading column controls the passage of the organic material and air during the loading process, such that it will close when organic material is being loaded into the loading column. After the air is removed from the organic material, the valve will open to allow the organic material to pass into the disaggregator 400. Smoke exhaust from the thermal propeller 200 flows into the loading column 300 through smoke exhaust 110.
  • the Archimedes' screw moves the organic material into fuser tubes to undergo the molecular disaggregation process and produce Syngas, Synoil, and/or Carbon.
  • the fuser tubes are housed within a furnace that is heated by the thermal propeller 200.
  • the fuser tubes may be made or formed, at least partially, of a metal alloy to promote the molecular disaggregation process.
  • the fuser pipes may be integral or may be formed from a plurality of sections joined, for example, by ceramic fiber gaskets.
  • carbon is separated from the liquid and gaseous hydrocarbons. The carbon exits the disaggregator 400 through port or exit 140.
  • the thermal propeller 200 has an automatic fuel loader that automatically loads, with flow modulation, the fuel for the operation of the thermal propeller.
  • the fuel can be carbon produced by the system itself or it can be other material of organic nature.
  • An Archimedes' screw moves the fuel into the thermal propeller 200, which produces and supplies thermal energy to the disaggregator 400, namely the fuser tubes, so the disaggregator 400 can carry out the molecular disaggregation process along with an ionization process.
  • a junction cube 600 is connected between thermal propeller 200 and the furnace of the disaggregator 400.
  • the junction cube 600 also allows the entrance of the fumes from the thermal propeller.
  • the junction cube 600 is formed by a chamber which is lined with refractory materials. When the refractory materials are constantly heated at a temperature between 1,200/1,400 °C, they become a thermal flywheel, which enables total catalytic effect upon them. Fumes or smoke from the thermal propeller enter the junction cube through entrance 130 and are transported through the furnace 400 and then to the loading column through the smoke exhaust 110.
  • the condenser is permeated by a chamber through which cold water runs, which cools the gases and causes the condensation of the Synoil.
  • the flow of cold water may be used for the thermal exchange with the exiting gases so that the part that can be condensed (Synoil) will be cooled and flow to the bottom of the condenser towards the exit point.
  • Synoil exits through port or exit 150 and enters a storage tank. Syngas exits the system at port 160 and is pumped into a storage tank.
  • the thermal propeller has a loader and a body.
  • the loader has fuel tank 210 that has an agitator 212 within it and motor 214 for moving the agitator 212, an Archimedes screw 220 and a motor 222 for rotating the Archimedes screw 220.
  • the Archimedes screw 220 moves solid fuel such as carbon, wood chips, municipal solid waste, agricultural waste, medical waste, sludges, etc. (i.e., generally organic materials having around 25% moisture or less), into the body of the thermal propeller 200.
  • the thermal propeller body has two lower chambers 240, 250 and a pyrolysis and combustion (gas oxidation) chamber 260 having catalytic walls.
  • the lower chamber 240 is under primary fuser slab 242 and is connected to lower chamber 250, which is under secondary fuser slab 252.
  • the fuser slabs 242, 252 have very heavy mass and heats up to a temperature between 350/450°C. At these temps, the fuel material on the fuser slabs is disaggregated to produce synthesis gas.
  • the fuel enters the thermal propeller 200 at a stoichiometric air carburetor 230, which has a turbine driven fan 232.
  • the carburetor 230 is connected to lower chamber 240 and combustion chamber 260.
  • the carburetor 230 is supplied with valves which measure out/choke the flow of air into the chambers 240, 260. The measuring out of air is meticulous as the air which will flow under the primary fuser slab 252 will be, at any rate, much less than the total oxidation gases that exit the holes 266 that are placed above, high up inside the combustion chamber 260.
  • the air regulation takes place by means of an oxygen sensor/detector placed inside the combustion chamber 260 and by means of an on-board computer which establishes the movement of the air choke valve.
  • Combustion preferably operates at temperatures of 1,200 - 1,500°C in perfect stoichiometry.
  • an initial amount of material for example 5kg, is placed on the primary fuser slab or plate 242, and a combustible material such as cotton soaked in gasoline is placed onto the primary fuser slab.
  • the fan 232 is then started and once ignition is achieve additional material is added via the loader.
  • Other methods of initiating combustion may be used with the present invention.
  • the turbine driven fan 232 supplies stoichiometric conditioned air through the carburetor 230 with a perfect stoichiometric ratio value for carburation of synthesis gases produced by the molecular disaggregation or pyrolysis process which takes place once the fuel is deposited on the fuser slabs 242, 252.
  • the measured out air coming out of the carburetor 230 will flow into the chamber 240 under the primary fuser slab 242, which has apertures or little holes 243 that allow the exit of the air under the fuel. It permits the creation of gases in partial oxygen deficiency.
  • a motor 248 is coupled to a pair of shafts 244, 254 by way of a transmission chain to cause the shafts 244, 254 to rotate simultaneously.
  • the shaft 244 extends through the primary fuser slab 242 and is connected to an agitator 246.
  • the shaft 254 extends through secondary fuser slab 252, which has holes 253 and is connected to agitator 256.
  • Solid fuel (carbon, wood chips, etc.) is moved onto the primary fuser slab 242 in the pyrolysis and combustion chamber 260 with Archimedes screw 220.
  • the agitator 246 mixes the fuel on the primary fuser slab to ensure a better exposure of the material to the heat which disaggregates the fuel and also moves partially processed fuel onto the secondary fuser slab.
  • the agitator 256 mixes the partially processed fuel on the secondary fuser slab and provides automatic unloading of the final inorganic ash into pit 270, from which the ash can be removed to a collection bucket located outside the thermal propeller 200.
  • the pyrolysis and combustion chamber 260 has fuser walls 264, a lid 262 and insulation refractory materials/stones 268 outside the fuser walls 264.
  • the fuser walls 264 are made of refractory material, for example, a mix of two or more of alumina, silicon, carbide and corundum, etc., and operate at a temperature up to 1,500 °C to irradiate the material which lays on or is otherwise positioned about the fuser slabs 242, 252.
  • the refractory materials are used to ensure thermal insulation and are made from various metal oxide powders, which give a high level of elasticity in the heating phase and high heat resistance at temperatures peaking at 2,400°C.
  • the four fuser walls 264 i.e., the four sides of the chamber, can be easily substituted by removing the lid 262.
  • the lid 262 is removed when extraordinary maintenance is needed. Once the lid 262 is removed, the inside of the pyrolysis and combustion chamber will be accessible for maintenance work.
  • the fuser walls 264 have holes 266 for the entrance of the stoichiometric air from the carburetor 230.
  • the gases When the gases are oxidized, they create a whirl which will characterize the flame seen flowing inside the furnace to heat the fuser tubes.
  • the loading column 300 has a primary tank 310 and a secondary tank 340.
  • a pneumatic piston/valve 314 closes the material inlet opening 312 in an airtight manner once the primary tank 310 becomes full. The closing of the inlet 312 opening enables the creation of negative pressure inside the primary tank 310 by means of a turbine 316.
  • the loading column 300 has a pneumatic piston 320 held in position by a bridge 322.
  • the bridge 322 provides sufficient space to permit the piston 320 to ascend and descend.
  • the pneumatic piston 320 is connected to a vertical sliding and rotating shaft 332 that is connected to an unloading valve 330. Decent of the piston 320 opens the valve 330. Ascent of the piston 320 closes the valve 330.
  • the piston 320 rotates and is driven by electric motor 334, which is connected to the piston by a transmission pulley such as a rubber belt 366.
  • a transmission pulley such as a rubber belt 366.
  • the valve 330 provide for airtight closing of the secondary tank 340 once the loading is completed.
  • valve 330 With the valve 330 closed in an airtight manner, material is loaded into the primary tank via the entry point 312. Once the loading of material into the primary tank 310 is completed, the piston/valve 314 closes the entry point 312 in an airtight manner. A turbine 316 connected to the primary tank creates negative pressure inside the primary tank 310 to remove air from the organic material.
  • a gear motor 352 drives an Archimedes' screw 350 to move the material from the loading column 300 into the pyrodisaggregator 400.
  • the electric motor 352 is regulated by an inverter), which determines the most suitable speed of operation on the basis of the type of material which needs to be moved.
  • An agitator/stirrer 342 located at the bottom of the secondary tank 340 is driven by another gear motor to move the material so as to make it fall easily into the Archimedes' screw 350.
  • the Archimedes' screw 350 which moves the material into the disaggregator, is formed by spiral shaped sectors which rotate a full 360°. The spirals are detached one from the other but they are welded onto the drive shaft. This structure makes it so the drive shaft of the Archimedes' screw does not deform/warp when it operates at high temperatures.
  • the molecular pyrodisaggregator 400 has a furnace 410 connected to the junction cube 600.
  • the furnace 410 has one or more fuser tubes 420 within it.
  • the fuser tubes or pipes 420 are formed from a metal alloy that emits high quantities of ions within the fuser tubes during the pyrolysis process.
  • the number of fuser tubes 420 may vary depending on the size of the plant.
  • An Archimedes' screw 430 is positioned in the fuser tube 420 for moving materials inside the fuser tube 420 needing to be processed downstream.
  • a furnace lid 412 is placed on the furnace 410 after the fuser tubes have been placed inside the furnace.
  • a ceramic gasket may be used as a seal between the lid 412 and the furnace walls.
  • Chamber or space 440 between the fuser tubes and the furnace wall allow hot fumes from the thermal propeller 200 to circulate/rotate around the fuser tubes 420.
  • the hot fumes from the thermal propeller 200 enter the space 440 through entrance 122.
  • An exit 442 for the fumes that have been used to heat the fuser tubes is provided.
  • a plurality of automatic extractors may be provided to remove dust produced by the thermal propeller 200 from the furnace 400.
  • Materials within the furnace 420 are moved by the Archimedes screw 430 toward exit 140 for carbon-metals-inert materials and exit 450 for gases.
  • the fuser pipes are heated by a heat source (the thermal propeller in some embodiments) which generates heat by combustion.
  • the molecular disaggregation process begins when the fuser tubes reach a temperature of about 200°C and ends once the organic material, having reached a temperature of about 350°C, sublimates completely and reaches the ends of the fuser tubes in a solid (carbon) and hydro gaseous (Synoil and Syngas) form.
  • the solid materials exiting through exit 140 are moved toward a separator which separates the various products into separate containers.
  • the solid materials Prior to moving into the separator, the solid materials may be conveyed to an airtight heat exchanger to undergo a cooling process to prevent spontaneous combustion at high temperatures due to the presence of oxygen.
  • the solid materials may be used as fuel for the thermal propeller 200 or other industrial purposes.
  • the gases exiting through exit 450 proceed to the condenser 500 for cooling.
  • Example organic materials that may be used as feedstock for an embodiment of the pyrodisaggregator include plastics, tires, certain woods, agricultural waste (e.g. coconut shells), bamboo and other organic materials known to those skilled in the art to disaggregate into outputs such as syngas, synoil and carbon black.
  • the condenser 500 has an entrance dome 512 through which gases from the molecular pyrodisaggregator 400 enter the condenser 500.
  • the entry point is covered by a cold water chamber 510.
  • Connection flange 514 between the chamber 510 and the molecular pyrodisaggregator 400 are connected by means of an insulated pipe.
  • the gases reaching the condenser are hot (300-400°C) and so the hydrocarbons (oil of synthesis) are still in gaseous form.
  • the condenser 500 needs to cool the gases and enable the condensation of the oil of synthesis (it becomes liquid).
  • the circular entrance dome 512 is covered by a cold water chamber 510. By means of a hydraulic pump, the water circulates into all of the cooling circuit. As the oil condenses, it falls into the hopper 520 while the Syngas, which cannot be condensed, h continues its advance to the columns 530. After passing through the columns 530, the syngas is suctioned by turbine/aspirator 560 to be moved into Syngas collection tanks and light hydrocarbons are collected in hopper 550,.
  • the cooling circuit has a pair of columns 530 connected by a connection manifold 540.
  • the columns 530 each have a channel 536 that allows the gases to move along a long and cooled path and in doing so they lose all the liquid part which unloads into the hoppers 520, 550.
  • An air-lock spacer 534 is inside the column 530 where the water which cools the Syngas circulates. Spirals, cochlea or other batting 532 inside the columns 530 slow down the flow of the Syngas. This allows the gases to cool down properly by reaching room temperature. When this happens, all the condensable portions will have already been condensed and the various kinds of Syngas will be dry and clean.
  • the main hopper 520 collects the vast majority of the oil which has condensed. It also refines the condensing process by moving the gas into the column.
  • Suction/aspiration point 522 is provided for the oil of synthesis. The oil is suctioned by means of a pump and sent to a collection tank.
  • Secondary hopper 550 collects the light hydrocarbons which move along with the Syngas, as they are lighter than the oils in the primary hopper 520.
  • Suction/aspiration point 552 is provided for suction of light hydrocarbons by means of a pump. They then are sent to a collection tank.
  • Turbine/aspirator 560 moves the Syngas, cleaned from any oil and thus dry, into a storage tank, where it is ready to be used for all intended purposes.
  • a titanium/platinum ion catalyst junction cube 600, or "C.I.T. Cube,” in accordance with an embodiment of the present disclosure is described with referenced to FIG. 6 .
  • the C.I.T. Cube uses composition materials TiO6, TiO2 and PTO2 mixed in Al2O3 to transform or eliminate harmful exhaust gas generated by endothermic engines.
  • the C.I.T. Cube treats toxic - noxious exhaust gas emanating from endothermic engines or by industrial processes and in an embodiment emits only H2, CO2 and H2O.
  • the C.I.T. Cube is a parallelepiped that generally is inserted between a thermal propeller (that regardless the type of fuel that is used produces heat above 1000 ° C), and a heat exchanger.
  • the heat produced before going to the thermal exchange (be it air/water, steam, diathermic oil heat exchanger or a cooking furnace or a dryer etc.) accumulates in a labyrinth made of refractory bars made with types of metals in the form of oxides such as Ti06 (titanium hexaoxide), Ti02 (titanium dioxide), PtO2 (platinum dioxide).
  • the C.I.T. Cube 600 has a housing 610 formed of metal sheets and internally insulated with isolating refractory materials.
  • the C.I.T. Cube is connected to a thermal propeller at entry or port 620.
  • Smoke or exhaust generated by an endothermic engine or an exhaust with other polluting elements as above described enters the C.I.T. Cube through entry or port 630.
  • a second entry or port 640 is provided for smoke/exhaust generated by another endothermic engine or for other polluting elements as above described.
  • a plurality of titanium/platinum ion boards 650 are positioned with the C.I.T. Cube 600.
  • the titanium/platinum boards 650 act as the catalyst.
  • Exit point 660 is provided for processed smoke that will proceed toward the heat exchanger.
  • the hydraulic disc filter is used to clean/purify the flue/exhaust emissions of boilers/heaters and furnaces, and also for the purification of gas of synthesis, ambient air, etc.
  • the hydraulic net filter could be connected to Syngas exit 160 in FIG. 1 .
  • the filter 700 has a plurality of rotating discs 722 that create centrifugal force.
  • the liquid will create a circular net in which the flue/exhaust gas, as they pass through the net, will be purified from all the particulate which travels alongside of them, and also from all the acid molecules such as HCL, H2SO4, etc.
  • the particulate will be consequently captured as mud/sludge, in a designated receptacle/site, while the acids will be neutralized with basic powders or electrolytic equipment.
  • the hydraulic net filter 700 of the present disclosure has a metallic tower 720 that rests on a tank 760 which contains, depending on the required needs, either water or oil.
  • the tower 720 is connected to a series of compartments, compartment 710 on the side from which the air flow enters the tower 720 and compartments 730, 740 on the side from which the air flow exits the tower 720.
  • the tower 720 contains a rotating shaft 724 with discs 722.
  • the flue or exhaust gas (referred to herein as "gas flow”) needing purification accesses the hydraulic net filter 700 through port or entrance 712 in compartment 710 and completes a 180° revolution, i.e., it travels from the port 712 near the top of the compartment 710 down to the bottom of the compartment 710 to a port or opening between the compartment 710 and the tower 720. Through this maneuver it loses the great majority of dry particulate, which drops into the compartment or drawer 714 from which it is periodically removed. Next, as the gas flow enters the lower portion of the tower 720 it will flow up into the disc area of the tower 720. In the tower 720, a hydraulic pump 762 pumps water/oil through a manifold 730 directly onto the discs 722.
  • a motor 726 connected to the shaft 724 rotates the shaft 724, and hence the discs 722, thereby generating a centrifugal effect. Because of the centrifugal effect, the discs 722 will create a hydraulic net which will hit the walls of the tower.
  • the hydraulic filters formed by the centrifuge created by the discs will travel at a speed which will vary around 70/100 ml per second. This way no particle moved by the gas flow (regardless of its speed) will be able to escape capture by the hydraulic net.
  • the particulate and the hydraulic liquid from the tower 720 will fall in the tank 760 underneath the tower 720 where the liquid will decant the particulate into the compartment 780 from which it will later be removed, whether manually or automatically.
  • a cooling liquid basin 750 Separated from the tank 760 by a diagonal wall 770 is a cooling liquid basin 750, which has an entry way 752 and an exit 754.
  • the cooling liquid basin has a cooling liquid in the event that the gas flow, which is hot, may cause excess evaporation of process water.
  • the process liquid (water/oil), which is stored in stocking tank 760 and flows up the manifold 730 does not need to be substituted as only the mud/sludge will be removed.
  • the tank 760 has a float 764 for the automatic topping up/refilling of the process liquid to compensate for the water evaporation.
  • the tank 760 has an inspection door or lid 790 for inspecting or performing maintenance on the tank 760 or any of the components within it.
  • the inspection door 790 also may be used to load basic powders used to regulate the PH of the process liquid.
  • the gas flow after traveling up the metallic depuration tower 720 flows into and through compartment 730 and then into and through compartment 740, from which it exits the filter 700 at exit 742, after having left behind in the circuit through compartments 730, 740 possible residual process liquid drops.
  • the gas flow then will be released, either in the atmosphere - when it is flue/exhaust gas, or in a stocking chamber - when it is technical or fuel gas.
  • a hydraulic network by means of centrifugal wheels/discs water streams, traveling up to and beyond the speed of 100 linear meters per second, comprise the network.
  • This system can operate using liquids which will rarely, if ever, need to be changed.
  • the mud/sludge can be removed without draining or substituting the processing liquid.
  • the system can be used to cleanse/purify highly flammable gas flows. Additionally, the system carries out its process in a closed circuit. Still further, the system can perform with little electrical usage as there are only two small motors that need to be powered.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
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  • Processing Of Solid Wastes (AREA)

Claims (13)

  1. Système de désagrégation par pyrolyse moléculaire (100) comprenant :
    un appareil de désagrégation par pyrolyse (400), ledit appareil de désagrégation par pyrolyse (400) comprenant :
    un four (410), ledit four (410) ayant une chambre de four (440) ;
    un tube (420) au sein de ladite chambre de four (440) ;
    une vis d'Archimède (430) au sein dudit tube (420) configurée pour déplacer du matériau à désagréger à travers ledit tube (420) ;
    une première sortie de four (140) configurée pour faire sortir des matériaux inertes dudit tube (420) ;
    une deuxième sortie de four (450) configurée pour faire sortir des gaz dudit tube (420) ; et
    une troisième sortie de four (442) configurée pour faire sortir des fumées circulant à travers ladite chambre de four (440) ; dans lequel
    ledit tube (420) est raccordé à ladite première sortie (140) et à ladite deuxième sortie (450) ;
    le système de désagrégation par pyrolyse moléculaire (100) comprenant :
    une colonne de chargement (300) raccordée audit appareil de désagrégation par pyrolyse (400) configurée pour charger des matériaux à désagréger dans ledit tube (420) situé dans ledit four (410) ;
    un appareil source de fumées chaudes (200) raccordé audit four (410) afin de faire entrer des fumées chaudes dans ladite chambre de four (440) et faire circuler lesdites fumées chaudes au sein de ladite chambre de four (440) autour dudit tube (420) ; et
    un condenseur (500) raccordé à ladite deuxième sortie (450) ;
    dans lequel ledit condenseur (500) comprend :
    un dôme d'entrée (512) raccordé à ladite deuxième sortie (450) depuis ledit four (410) pour recevoir des gaz dudit appareil de désagrégation par pyrolyse (400) ;
    une chambre d'eau froide (510) entourant ledit dôme d'entrée (512) destinée à refroidir lesdits gaz reçus dudit appareil de désagrégation par pyrolyse (400) ;
    une trémie primaire (520) raccordée audit dôme d'entrée (512) destinée à collecter de l'huile condensée à partir desdits gaz reçus dudit appareil de désagrégation par pyrolyse (400) ;
    dans lequel le système de désagrégation par pyrolyse moléculaire (100) est caractérisé en ce que le condenseur (500) comprend :
    des première et seconde colonnes de condenseur verticales (530) destinées à établir un chemin refroidi pour le gaz s'écoulant dans lesdites colonnes de condenseur (530), chaque colonne de condenseur (530) comprenant :
    un canal (536) à travers lequel des gaz s'écoulent ; et
    un espace de poche d'air (534) pour de l'eau utilisée pour refroidir des gaz au sein dudit canal (536) ; un collecteur de raccordement (540) raccordant ladite première colonne de condenseur (530) à ladite seconde colonne de condenseur, afin qu'un gaz s'écoule dudit dôme d'entrée dans et à travers ladite première colonne de condenseur (530) puis à travers ledit collecteur de raccordement (540) puis à travers ladite seconde colonne de condenseur (530) ;
    une trémie secondaire (550) raccordée à ladite deuxième colonne de condenseur (530) pour recevoir des hydrocarbures légers de ladite seconde colonne de condenseur (530) ; et
    un aspirateur (560) destiné à déplacer du gaz de synthèse dudit condenseur dans un réservoir de stockage.
  2. Système de désagrégation par pyrolyse moléculaire (100) selon la revendication 1, dans lequel ledit condenseur (500) comprend en outre :
    une pluralité de spirales au sein dudit canal (536) dans au moins l'une desdites première et seconde colonnes de condenseur (530) pour ralentir un écoulement de gaz au sein de ladite colonne de condenseur (530).
  3. Système de désagrégation par pyrolyse moléculaire (100) selon l'une quelconque des revendications 1 et 2, dans lequel ledit appareil source de fumées chaudes (200) comprend :
    une chambre de combustion et pyrolyse (260) formée par :
    au moins une paroi latérale ;
    une dalle de fusion primaire (242) et une dalle de fusion secondaire (252) formant un fond de ladite chambre de combustion et pyrolyse, ladite dalle de fusion primaire étant positionnée pour recevoir du combustible solide de ladite colonne de chargement et ladite dalle de fusion secondaire (252) étant positionnée pour recevoir du combustible solide de ladite dalle de fusion primaire (242) ; et
    un couvercle destiné à fermer ladite chambre de combustion et pyrolyse.
  4. Système de désagrégation par pyrolyse moléculaire (100) selon la revendication 3, dans lequel ledit appareil source de fumées chaudes (200) comprend en outre :
    un premier brasseur (246) destiné à déplacer du combustible solide sur ladite dalle de fusion primaire (242) ; et
    un second brasseur (256) destiné à déplacer du combustible solide sur ladite dalle de fusion secondaire (252).
  5. Système de désagrégation par pyrolyse moléculaire (100) selon la revendication 3, dans lequel ledit appareil source de fumées chaudes (200) comprend en outre :
    un carburateur à air stoechiométrique (230) raccordé à ladite chambre de combustion et pyrolyse (260).
  6. Système de désagrégation par pyrolyse moléculaire (100) selon la revendication 5, dans lequel ledit carburateur à air stoechiométrique (230) comporte une sortie (266) dans ladite chambre de combustion et pyrolyse (260) dans une portion supérieure de ladite chambre de combustion et pyrolyse (260).
  7. Système de désagrégation par pyrolyse moléculaire (100) selon l'une quelconque des revendications 5 et 6, dans lequel ledit appareil source de fumées chaudes (200) comprend en outre :
    un ventilateur entraîné par turbine (232) raccordé audit carburateur à air stoechiométrique (230).
  8. Système de désagrégation par pyrolyse moléculaire (100) selon l'une quelconque des revendications 5 à 7, dans lequel ledit appareil source de fumées chaudes (200) comprend :
    une première chambre inférieure (240) en dessous de ladite dalle de fusion primaire (242), dans lequel une pluralité de trous d'air (243) s'étend à travers ladite dalle de fusion primaire (242), dans lequel ledit carburateur à air stoechiométrique (230) est raccordé à ladite première chambre inférieure (240).
  9. Système de désagrégation par pyrolyse moléculaire (100) selon l'une quelconque des revendications 5 et 8, dans lequel ledit appareil source de fumées chaudes (200) comprend en outre :
    une sortie de déchargement de cendre par le bas (270).
  10. Système de désagrégation par pyrolyse moléculaire (100) selon l'une quelconque des revendications 8 à 9, dans lequel ledit appareil source de fumées chaudes comprend :
    une seconde chambre inférieure (250) en dessous de ladite dalle de fusion secondaire (252), dans lequel une pluralité de trous d'air (253) s'étend à travers ladite dalle de fusion secondaire (252), dans lequel ladite seconde chambre inférieure (250) est raccordée à ladite première chambre inférieure (240).
  11. Système de désagrégation par pyrolyse moléculaire (100) comprenant :
    un appareil de désagrégation par pyrolyse (400), ledit appareil de désagrégation par pyrolyse (400) comprenant :
    un four (410), ledit four (410) ayant une paroi de four définissant une chambre au sein dudit four (410) ;
    un tube (420) au sein de ladite chambre de four ;
    un canal (440) au sein de ladite chambre de four entourant ledit tube (420) ;
    une vis d'Archimède (430) au sein dudit tube (420) destinée à déplacer du matériau à désagréger à travers ledit tube (420) ;
    une première sortie (140) dudit tube (420) configurée pour des matériaux inertes provenant dudit tube (420) ;
    une deuxième sortie (450) dudit tube de fusion (420) pour des gaz provenant dudit tube de fusion (420) ; et
    une troisième sortie (442) pour des fumées circulant à travers ledit canal situé dans ledit four (410) ;
    un organe de chargement (300) raccordé audit appareil de désagrégation par pyrolyse (400) destiné à charger des matériaux à désagréger dans ledit tube de fusion (420) dans ledit four (410) ;
    une source de fumées chaudes (200) raccordée audit four (410), dans lequel des fumées chaudes provenant de ladite source de chaleur (200) circulent dans ledit canal (440) est ledit four autour dudit tube de fusion (420) ; et
    un condenseur (500) raccordé à ladite deuxième sortie (450) ;
    dans lequel ledit condenseur (500) comprend :
    une structure d'entrée (512) raccordée à ladite deuxième sortie (450) depuis ledit four (410) destinée à recevoir des gaz provenant dudit appareil de désagrégation par pyrolyse (400) ;
    une chambre d'eau froide (510) entourant ladite entrée (512) destinée à refroidir lesdits gaz reçus dudit appareil de désagrégation par pyrolyse (400) ; dans lequel le système de désagrégation par pyrolyse moléculaire (100) est caractérisé en ce que le condenseur comprend :
    des première et seconde colonnes de condenseur (530) chacune destinée à prouver un chemin refroidi pour un gaz s'écoulant dans lesdites colonnes de condenseur (530), chaque colonne de condenseur (530) comprenant :
    un élargissement au sein de chaque dite colonne de condenseur (530) destiné à ralentir un écoulement de gaz au sein de ladite colonne de condenseur (530) ;
    un espace de poche d'air (534) au sein de chaque dite colonne de condenseur (530) pour faire circuler de l'eau utilisée pour refroidir du gaz ;
    un collecteur de raccordement (540) raccordant ladite première colonne de condenseur (530) à ladite seconde colonne de condenseur (530), dans lequel un gaz provenant de ladite structure d'entrée (512) s'écoule dans et à travers ladite première colonne de condenseur (530) puis à travers ledit collecteur de raccordement (540) puis à travers ladite seconde colonne de condenseur (530) ;
    une trémie primaire (520) raccordée à ladite structure d'entrée (512) et à ladite première colonne de condenseur (530) pour collecter de l'huile condensée à partir desdits gaz reçus dudit appareil de désagrégation par pyrolyse (400) ;
    une trémie secondaire (550) raccordée à ladite seconde colonne de condenseur (530) pour recevoir des hydrocarbures légers reçus de ladite seconde colonne de condenseur (530).
  12. Système de désagrégation par pyrolyse moléculaire (100) selon la revendication 11, dans lequel ledit condenseur (500) comprend en outre :
    un aspirateur (560) destiné à déplacer du gaz de synthèse dudit condenseur (500) dans un réservoir de stockage.
  13. Système de désagrégation par pyrolyse moléculaire (100) selon la revendication 11, dans lequel ladite structure d'entrée comprend un dôme.
EP16724595.0A 2015-04-30 2016-04-29 Four à pyrolyse Active EP3289050B1 (fr)

Applications Claiming Priority (11)

Application Number Priority Date Filing Date Title
ITBS20150072 2015-04-30
ITUB20152288 2015-07-03
ITUB20152287 2015-07-06
ITUB20152476 2015-07-10
ITUB20152492 2015-07-10
ITUB2015A005217A ITUB20155217A1 (it) 2015-10-15 2015-10-15 Propulsore termico a combustibile solido
ITUB2015A004810A ITUB20154810A1 (it) 2015-10-15 2015-10-15 Pirodisgregatore molecolare
ITUB2015A004809A ITUB20154809A1 (it) 2015-10-15 2015-10-15 Depuratore biogas
ITUB2015A005142A ITUB20155142A1 (it) 2015-10-15 2015-10-15 Filtro a rete idraulica
ITUB2015A005060A ITUB20155060A1 (it) 2015-10-15 2015-10-15 Sistema catalizzatore a ioni di platino/titanio
PCT/EP2016/059696 WO2016174247A1 (fr) 2015-04-30 2016-04-29 Four de pyrolyse

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Publication Number Publication Date
EP3289050A1 EP3289050A1 (fr) 2018-03-07
EP3289050B1 true EP3289050B1 (fr) 2019-06-19

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US (1) US10899967B2 (fr)
EP (1) EP3289050B1 (fr)
CA (1) CA2984198A1 (fr)

Cited By (1)

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CN113072964A (zh) * 2021-04-06 2021-07-06 无锡上工锅固废利用科技有限公司 生物质卧式旋芯炭化炉

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CN110396584A (zh) * 2018-04-24 2019-11-01 佛山市嘉懿行农业科技有限公司 一种高精度气氛保护程控回火炉用炉体
CN111826178A (zh) * 2020-07-17 2020-10-27 安徽林农时代科技有限公司 一种卸温出炭装置

Family Cites Families (70)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1467509A (en) * 1920-02-19 1923-09-11 Skinner Lewis Bailey Furnace apparatus
GB176025A (en) * 1920-09-04 1922-03-06 Lewis Bailey Skinner Improvements in apparatus for conducting furnacing operations
GB368291A (en) 1930-10-24 1932-02-24 Ig Farbenindustrie Ag Improvements in the conversion of hydrocarbons at higher temperatures
US2225199A (en) * 1939-04-28 1940-12-17 Colorado Iron Works Co Multiple hearth calcining furnace
US2475639A (en) * 1944-07-05 1949-07-12 Rainwater Harold Spray evaporator with dome condenser
US2525973A (en) 1946-11-19 1950-10-17 Allied Chem & Dye Corp Apparatus for feeding solid material
US3232341A (en) * 1960-02-01 1966-02-01 Garrett Corp Condenser
US3470068A (en) * 1966-10-12 1969-09-30 Salem Brosius Inc Methods and apparatus for the continuous treatment of non-caking coal and other discrete materials
US3625778A (en) 1970-06-03 1971-12-07 Ethyl Corp Heat-treating aluminum silicon alloy
US4009263A (en) 1974-02-15 1977-02-22 Shafer Laverne Energized cobalt-containing animal feed
GB1501729A (en) 1974-05-06 1978-02-22 Redker Young Processes Inc Conversion of organic waste material
US3881431A (en) * 1974-06-19 1975-05-06 Sabatino Disabatino Incinerator
US3958920A (en) * 1975-06-03 1976-05-25 Rust Engineering Company System for controlling the operation of a multiple hearth furnace
US4030877A (en) * 1975-11-26 1977-06-21 Robinson Philip W Furnace waste gas heat recovery device and method of using same
US4027602A (en) * 1976-02-13 1977-06-07 Mott James R Combustion system
US4095426A (en) * 1976-08-27 1978-06-20 Rhodes William A Turbine and method of using same
US4182246A (en) * 1978-01-16 1980-01-08 Envirotech Corporation Incineration method and system
DE2922041A1 (de) * 1979-05-30 1980-12-04 Herko Pyrolyse Recycling Reaktor fuer die pyrolyse von abfallstoffen
US4248604A (en) * 1979-07-13 1981-02-03 Texaco Inc. Gasification process
US4247367A (en) * 1979-11-16 1981-01-27 Reilly Bertram B Apparatus for solid waste pyrolysis
US4385567A (en) * 1980-10-24 1983-05-31 Solid Fuels, Inc. Solid fuel conversion system
US4516302A (en) 1981-07-31 1985-05-14 Ingersoll-Rand Company Field replaceable screw conveyor inserts
US4838341A (en) 1983-12-06 1989-06-13 Allied Signal Inc. Production of low temperature aluminum based brazing alloys
US4820382A (en) * 1985-03-15 1989-04-11 Union Oil Company Of California Method and apparatus for removing solids from an upwardly moving bed chamber
US4838183A (en) * 1988-02-11 1989-06-13 Morse Boulger, Inc. Apparatus and method for incinerating heterogeneous materials
JPH062726Y2 (ja) * 1989-06-23 1994-01-26 住友軽金属工業株式会社 ねじり板挿入管を有するミスト回収装置
EP0427899A1 (fr) 1989-11-16 1991-05-22 Société GOMACRIS S.A. Procédé de valorisation de déchets solides notamment d'ordures ménagères et dispositif pour sa mise en oeuvre
CA2045254C (fr) * 1991-06-21 1998-04-14 Christian Roy Traitement de residu de dechiquetage d'automobile par pyrolyse sous vide
US5747561A (en) 1992-10-14 1998-05-05 Smirnov; Aleksandr Vitalievich Solid surface modifier
US5376458A (en) 1992-11-30 1994-12-27 The United States Of America As Represented By The United States Department Of Energy Structural alloy with a protective coating containing silicon or silicon-oxide
US6171707B1 (en) 1994-01-18 2001-01-09 3M Innovative Properties Company Polymeric film base having a coating layer of organic solvent based polymer with a fluorinated antistatic agent
WO1996004409A1 (fr) 1994-08-01 1996-02-15 Franz Hehmann Traitement selectionne d'alliages legers et de produits hors d'equilibre
US5653183A (en) 1994-09-22 1997-08-05 Balboa Pacific Corporation Pyrolytic waste treatment system
US6537388B1 (en) 1996-08-23 2003-03-25 Alon, Inc. Surface alloy system conversion for high temperature applications
TW436597B (en) 1997-12-19 2001-05-28 Exxon Production Research Co Process components, containers, and pipes suitable for containign and transporting cryogenic temperature fluids
ATE416023T1 (de) 2000-12-18 2008-12-15 Conocophillips Co Schwefelrückgewinnungsverfahren
US6634781B2 (en) 2001-01-10 2003-10-21 Saint Gobain Industrial Ceramics, Inc. Wear resistant extruder screw
US6497187B2 (en) * 2001-03-16 2002-12-24 Gas Technology Institute Advanced NOX reduction for boilers
FI120909B (fi) * 2001-04-12 2010-04-30 Neste Oil Oyj Menetelmä hiilipitoisen materiaalin käsittelemiseksi
LU90766B1 (en) * 2001-04-25 2002-10-28 Wurth Paul Sa Method of operating a multiple hearth furnace
US6863878B2 (en) 2001-07-05 2005-03-08 Robert E. Klepper Method and apparatus for producing synthesis gas from carbonaceous materials
US20030118855A1 (en) 2001-12-21 2003-06-26 Santella Michael L. Aluminum alloys having improved surface properties and method of making same
AUPR982302A0 (en) * 2002-01-03 2002-01-31 Pax Fluid Systems Inc. A fluid flow controller
SE526673C2 (sv) 2003-08-28 2005-10-25 Sandvik Intellectual Property Användning av en metallförstoftningsresistent kopparlegering
US7083663B2 (en) 2003-10-30 2006-08-01 The Regents Of The University Of Michigan Active filtration of airborne contaminants employing heated porous resistance-heated filters
US7790316B2 (en) 2004-03-26 2010-09-07 Shin-Etsu Chemical Co., Ltd. Silicon composite particles, preparation thereof, and negative electrode material for non-aqueous electrolyte secondary cell
US7732059B2 (en) 2004-12-03 2010-06-08 Alcoa Inc. Heat exchanger tubing by continuous extrusion
US8501668B2 (en) 2005-04-29 2013-08-06 University Of Rochester Drug screening via nanopore silicon filters
CA2634252A1 (fr) 2005-12-21 2007-07-05 Exxonmobil Research And Engineering Company Materiau resistant a la corrosion pour encrassement reduit, composant de transfert thermique ameliore en termes de resistance a la corrosion et a l'encrassement et procede pour reduire l'encrassement
ATE500725T1 (de) 2006-05-10 2011-03-15 Fraunhofer Ges Forschung Schneidevorrichtung
WO2007136148A1 (fr) 2006-05-24 2007-11-29 Sk Energy Co., Ltd. Dispositif de purification de gaz d'échappement destiné à un moteur diesel présentant une ligne de recirculation de gaz d'échappement
US9045693B2 (en) 2006-12-26 2015-06-02 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof
US20090007484A1 (en) * 2007-02-23 2009-01-08 Smith David G Apparatus and process for converting biomass feed materials into reusable carbonaceous and hydrocarbon products
CA2731803A1 (fr) 2007-07-25 2009-01-29 John Patton Appareil, systeme, et procede de traitement de gaz d'hydrogene
CN101849306B (zh) 2007-09-06 2013-06-12 佳能株式会社 锂离子储存/释放材料的制备方法、锂离子储存/释放材料、使用该材料的电极结构体和储能器件
WO2009061954A1 (fr) 2007-11-06 2009-05-14 Quantumsphere, Inc. Système et procédé de synthèse d'ammoniac
DE102007053284A1 (de) 2007-11-08 2009-05-20 Esk Ceramics Gmbh & Co. Kg Fest haftende siliciumnitridhaltige Trennschicht
EP2220453A1 (fr) 2007-12-21 2010-08-25 Doty Scientific Inc. Récupérateur de composés gaz-gaz à haut rendement et compact, avec liquide intermédiaire
ITBS20070212A1 (it) 2007-12-24 2009-06-25 Domenico Tanfoglio Macchina per la produzione a ciclo continuo di alcool metilico (ch30h) da biomasse
MX2010010859A (es) * 2008-04-03 2010-11-01 Univ North Carolina State Dispositivos autotermicos y moviles de torrefaccion.
FR2945817B1 (fr) 2009-05-25 2013-09-27 Francois Hustache Nouveau dispositif pour la gazeification de dechets organiques, et procede de mise en oeuvre de ce dispositif
WO2011075836A1 (fr) 2009-12-23 2011-06-30 Arise Technologies Corporation Production d'un gaz vecteur pour la déposition en phase gazeuse à partir d'un alliage métal-silicium eutectique et hypo-eutectique
US9112224B2 (en) 2010-06-30 2015-08-18 Semiconductor Energy Laboratory Co., Ltd. Energy storage device and method for manufacturing the same
US8795476B2 (en) * 2010-09-24 2014-08-05 John Flottvik Charcoal reactor system
US8877468B2 (en) * 2010-09-24 2014-11-04 Anaergia Inc. Method for converting biomass to methane or ethanol
US20120237693A1 (en) 2011-03-17 2012-09-20 Applied Materials, Inc. In-situ clean process for metal deposition chambers
FR2974858A1 (fr) 2011-05-04 2012-11-09 Peugeot Citroen Automobiles Sa Procede de fabrication d'une chemise equipant un cylindre d'un moteur thermique, pour vehicule automobile notamment
WO2013049665A2 (fr) * 2011-09-30 2013-04-04 Chevron U.S.A., Inc. Procédé de production d'une bio-huile compatible avec un courant de raffinage à partir d'une charge d'alimentation lignocellulosique
AU2015203118A1 (en) 2012-11-15 2015-07-09 Kevin Lee Friesth Quintuple-effect generation multi-cycle hybrid renewable energy system with integrated energy provisioning, storage facilities and amalgamated control system
US20140259895A1 (en) 2013-03-14 2014-09-18 Bonfire Biomass Conversions, LLC Mobile Pelletizing System

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113072964A (zh) * 2021-04-06 2021-07-06 无锡上工锅固废利用科技有限公司 生物质卧式旋芯炭化炉
CN113072964B (zh) * 2021-04-06 2021-12-21 无锡上工锅固废利用科技有限公司 生物质卧式旋芯炭化炉

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